EP2190904A1 - Polymères réducteurs de traînée non poly(alpha-oléfiniques) dispersés - Google Patents

Polymères réducteurs de traînée non poly(alpha-oléfiniques) dispersés

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Publication number
EP2190904A1
EP2190904A1 EP08796916A EP08796916A EP2190904A1 EP 2190904 A1 EP2190904 A1 EP 2190904A1 EP 08796916 A EP08796916 A EP 08796916A EP 08796916 A EP08796916 A EP 08796916A EP 2190904 A1 EP2190904 A1 EP 2190904A1
Authority
EP
European Patent Office
Prior art keywords
substituted
radical
polymer
alkyl radical
particles
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP08796916A
Other languages
German (de)
English (en)
Other versions
EP2190904B1 (fr
Inventor
Timothy L. Burden
Ray L. Johnston
William F. Harris
Kenneth W. Smith
Wayne R. Dreher
Stuart N. Milligan
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Lubrizol Specialty Products Inc
Original Assignee
ConocoPhillips Co
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
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Application filed by ConocoPhillips Co filed Critical ConocoPhillips Co
Priority to EP20120156575 priority Critical patent/EP2457942A1/fr
Priority to EP14163613.4A priority patent/EP2752439B1/fr
Priority to PL08796916T priority patent/PL2190904T3/pl
Priority to DK14163613.4T priority patent/DK2752439T3/en
Publication of EP2190904A1 publication Critical patent/EP2190904A1/fr
Application granted granted Critical
Publication of EP2190904B1 publication Critical patent/EP2190904B1/fr
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J3/00—Processes of treating or compounding macromolecular substances
    • C08J3/02—Making solutions, dispersions, lattices or gels by other methods than by solution, emulsion or suspension polymerisation techniques
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2333/00—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical, or of salts, anhydrides, esters, amides, imides, or nitriles thereof; Derivatives of such polymers
    • C08J2333/04—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical, or of salts, anhydrides, esters, amides, imides, or nitriles thereof; Derivatives of such polymers esters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/0318—Processes
    • Y10T137/0391—Affecting flow by the addition of material or energy

Definitions

  • the present invention relates generally to drag reducing compositions comprising disperse polymer particles.
  • the present invention relates to drag reducing compositions comprising at least one drag reducing polymer made by emulsion polymerization.
  • a drag reducer is a composition capable of substantially reducing friction loss associated with the turbulent flow of fluid through a pipeline.
  • the role of these additives is to suppress the growth of turbulent eddies, which results in higher flow rate at a constant pumping pressure.
  • Ultra-high molecular weight polymers are known to function well as drag reducers, particularly in hydrocarbon liquids. In general, drag reduction depends in part upon the molecular weight of the polymer additive and its ability to dissolve in the hydrocarbon under turbulent flow.
  • a process for preparing a drag reducer comprises: (a) consolidating a plurality of initial particles comprising at least one polymer prepared via emulsion polymerization to thereby form one or more consolidated polymer structures; (b) decreasing the size of at least a portion of the consolidated polymer structures to thereby form a plurality of modified polymer particles; and (c) dispersing at least a portion of the modified polymer particles in a carrier fluid to thereby form the drag reducer.
  • a drag reducer comprising a plurality of particles comprising a non-polyalphaolefin polymer.
  • the particles are dispersed in a carrier fluid and have an average particle size in the range of from about 5 to about 800 micrometers.
  • the polymer has a weight average molecular weight of at least about 1 x 10 6 g/mol.
  • a method for reducing drag in a pipeline comprises: (a) introducing a drag reducer into a hydrocarbon-containing fluid to thereby form a treated hydrocarbon-containing fluid; and (b) flowing the treated hydrocarbon-containing fluid through a pipeline.
  • the drag reducer comprises a disperse phase comprising a plurality of particles comprising a non-polyalphaolefin polymer.
  • the particles have an average particle size in the range of from about 5 to about 800 micrometers.
  • the polymer has a weight average molecular weight of at least about 1 x 10' g/mol.
  • a drag reducing composition i.e.. a drag reducer
  • a drag reducer comprising a earner fluid and a plurality of particles comprising a non-polyalphaolefin polymer.
  • the non-polyalphaolefin polymer particles of the present invention can be prepared by first forming polymer particles via emulsion polymerization, followed by consolidating at least a portion of these initial particles into one or more consolidated polymer structures. Next, the size of the resulting consolidated polymer structures can be decreased, and the resulting modified polymer particles can be dispersed in the carrier fluid.
  • the drag reducer of the present invention can be employed to at least partially reduce the pressure drop associated with the turbulent flow of a hydrocarbon-containing fluid through a conduit (e.g., a pipeline).
  • the first step in producing the non-polyalphaolefin polymer particles of the present invention can be performed by preparing a non-polyalphaolefin polymer via emulsion polymerization.
  • This step can comprise the emulsion polymerization of a reaction mixture comprising one or more monomers, a continuous phase, at least one surfactant, and an initiation system.
  • the term "emulsion polymer” shall denote any polymer prepared via emulsion polymerization.
  • the resulting reaction product of the emulsion polymerization can be in the form of a latex composition comprising a disperse phase of non-polyalphaolefin particles (a.k.a., initial particles).
  • the continuous phase of the latex composition generally comprises at least one component selected from the group consisting of water, polar organic liquids (e.g., alcohol), and mixtures thereof.
  • the reaction mixture can also comprise a buffer. Additionally, as described in more detail below, the continuous phase can optionally comprise a hydrate inhibitor.
  • the non-polyalphaolefin polymer prepared via emulsion polymerization can comprise a plurality of repeating units of the residues of one or more of the monomers selected from the group consisting of:
  • R 1 is H or a Cl-ClO alkyl radical
  • R 2 is H, a C1-C30 alkyl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, a C6-C20 substituted or unsubstituted aryl radical, an aryl-substituted Cl-ClO alkyl radical, a -(CH2CH2O) X -R A or -(CH2CH(CH3)O) X -RA radical wherein x is in the range of from 1 to 50 and RA is H 5 a C1-C30 alkyl radical, or a C6-C30 alkylaryl radical; (B)
  • R 4 is H, a C1-C30 alkyl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, Cl, SO 3 , OR B , or COOR C
  • R B is H, a C1 -C30 alkyl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, a C6-C20 substituted or unsubstituted aryl radical, or an aryl-substituted Cl-ClO alkyl radical
  • Rc is H, a C1-C30 alkyl radical, a C5-C30 substituted or unsubstituted cycioalkyl radical, a C6-C20 substituted or unsub
  • R 3 - is H, a C1-C30 alkyl radical, or a C6-C20 substituted or unsubstituted aryl radical;
  • R 6 is H, a C1-C30 alkyl radical, or a C6-C20 substituted or unsubstituted aryl radical;
  • R 7 is H or a Cl-Cl 8 alkyl radical, and Rs is H, a Cl -C 18 alkyl radical, or Cl;
  • R 9 and Rio are independently H. a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
  • Rn and Rj 2 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
  • R 13 and R 14 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
  • Ri 5 is H, a C1 -C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
  • R 16 is H, a C1-C30 alkyl radical, or a C6-C20 aryl radical;
  • Rj 7 and Rig are independently H, a Cl-C 30 alkyl radical, a C6-C20 substituted or unsubstituted aryi radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
  • R 19 and R 20 are independently H. a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryi radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals.
  • the emulsion polymer of the present invention can comprise a non-polyalphaolefin polymer. Additionally, the emulsion polymer can comprise repeating units of the residues of C4-C20 alkyl, C6-C20 substituted or unsubstituted aryi, or aryl-substituted Cl-ClO alkyl ester derivatives of methacrylic acid or acrylic acid.
  • the emulsion polymer can be a copolymer comprising repeating units of the residues of 2-ethylhexyl methacrylate and the residues of at least one other monomer.
  • the emulsion polymer can be a copolymer comprising repeating units of the residues of 2-ethylhexyl methacrylate monomers and butyl acrylate monomers.
  • the emulsion pol>mer can be a homopolymer comprising repeating units of the residues of 2-ethylhexyl methacrylate.
  • the surfactant used in the above-mentioned reaction mixture can include at least one high HLB anionic or nonionic surfactant.
  • the term ⁇ LB number " ' refers to the hydrophile-lipophile balance of a surfactant in an emulsion.
  • the HLB number is determined by the methods described by W. C. Griffin in J Soc. Cosmet. Chem . 1. 311 (1949) and J. Soc. Cosmet. Chem.. 5, 249 (1954), which are incorporated herein by reference.
  • the term "high HLB' n shall denote an HLB number of 7 or more.
  • the HLB number of surfactants for use with forming the reaction mixture can be at least about 8, at least about 10, or at least 12.
  • Exemplar ⁇ ' high HLB anionic surfactants include, but are not limited to, high HLB alkyl sulfates, alkyl ether sulfates, dialkyl sulfosuccinates, alkyl phosphates, alkyl aryl sulfonates, and sarcosinates.
  • Suitable examples of commercially available high HLB anionic surfactants include, but are not limited to, sodium lauryl sulfate (available as RHODAPON LSB from Rhodia Incorporated, Cranbury.
  • Exemplary high HLB nonionic surfactants include, but are not limited to. high HLB sorbitan esters. PEG fatty acid esters, ethoxylated glycerine esters, ethoxylated fatty amines, ethoxylated sorbitan esters, block ethylene oxide/propylene oxide surfactants, alcohol/fatty acid esters, ethoxylated alcohols, ethoxylated fatty acids, alkoxylated castor oils, glycerine esters, linear alcohol ethoxylates. and alkyl phenol ethoxylates.
  • high HLB sorbitan esters PEG fatty acid esters, ethoxylated glycerine esters, ethoxylated fatty amines, ethoxylated sorbitan esters, block ethylene oxide/propylene oxide surfactants, alcohol/fatty acid esters, ethoxylated alcohols, ethoxylated fatty acids, alkoxy
  • Suitable examples of commercially available high HLB nonionic surfactants include, but are not limited to, nonylphenoxy and octylphenoxy poly(ethyleneoxy) ethanols (available as the IGEPAL CA and CO series, respectively from Rhodia, Cranbury. NJ), C8 to Cl 8 ethoxylated primary alcohols (such as RHODASURF LA-9 from Rhodia Inc.. Cranbury, NJ).
  • CI l to C15 secondary-alcohol ethoxylates available as the TERGITOL 15-S series, including 15-S-7, 15-S-9, 15-S-12, from Dow Chemical Company, Midland, MI
  • polyoxyethylene sorbitan fatty acid esters available as the TWEEN series of surfactants from Uniquema, Wilmington, DE
  • polyethylene oxide (25) oleyl ether available as SIPONIC Y-500-70 from Americal Alcolac Chemical Co., Baltimore, MD
  • alkylaryl polyether alcohols available as the TRITON X series, including X-IOO, X-165, X-305, and X-405, from Dow Chemical Company, Midland, MI).
  • the initiation system for use in the above-mentioned reaction mixture can be any suitable system for generating free radicals necessary to facilitate emulsion polymerization.
  • Possible initiators include, but are not limited to, per&ul fates (e.g., ammonium persulfate, sodium persulfate, potassium persulfate), pcroxy persulfates, and peroxides (e.g., tert-butyl hydroperoxide) used alone or in combination with one or more reducing components and/or accelerators.
  • Possible reducing components include, but are not limited to, bisulf ⁇ tes. metabisulfites, ascorbic acid, erythorbic acid, and sodium formaldehyde sulfoxylate.
  • Possible accelerators include, but are not limited to, any composition containing a transition metal having two oxidation states such as, for example, ferrous sulfate and ferrous ammonium sulfate.
  • known thermal and radiation initiation techniques can be employed to generate the free radicals.
  • any polymerization and corresponding initiation or catalytic methods known by those skilled in the art may be used in the present invention. For example, when polymerization is performed by methods such as addition or condensation polymerization, the polymerization can be initiated or catalyzed by methods such as cationic, anionic, or coordination methods.
  • the water can be purified water such as distilled or deionized water.
  • the continuous phase of the emulsion can also comprise polar organic liquids or aqueous solutions of polar organic liquids, such as those listed below.
  • the reaction mixture optionally can include a buffer.
  • the buffer can comprise any known buffer that is compatible with the initiation system such as, for example, carbonate, phosphate, and/or borate buffers.
  • the reaction mixture optionally can include at least one hydrate inhibitor.
  • the hydrate inhibitor can be a thermodynamic hydrate inhibitor such as, for example, an alcohol and/or a polyol.
  • the hydrate inhibitor can comprise one or more polyhydric alcohols and/or one or more ethers of polyhydric alcohols.
  • Suitable polyhydric alcohols include, but are not limited to, monoethylene glycol, diethylene glycol, tri ethylene glycol, monopropylene glycol, and/or dipropylene glycol.
  • Suitable ethers of polyhydric alcohols include, but are not limited to, ethylene glycol monomethyl ether, diethylene glycol monomethyl ether, propylene glycol monomethyl ether, and dipropylene glycol monomethyl ether.
  • the monomer, water, the at least one surfactant, and optionally the hydrate inhibitor can be combined under a substantially oxygen-free atmosphere that is maintained at less than about 1.000 ppmw oxygen or less than about 100 ppmw oxygen.
  • the oxygen-free atmosphere can be maintained by continuously purging the reaction vessel with an inert gas such as nitrogen and/or argon.
  • the temperature of the system can be kept at a level from the freezing point of the continuous phase up to about 60 0 C, in the range of from about 0 to about 45°C, or in the range of from 0 to 30 0 C.
  • the system pressure can be maintained in the range of from about 5 to about 100 psia, in the range of from about 10 to about 25 psia, or about atmospheric pressure. However, higher pressures up to about 300 psia can be necessary to polymerize certain monomers, such as diolefms.
  • a buffer can be added, if required, followed by addition of the initiation system, either all at once or over time.
  • the polymerization reaction is carried out for a sufficient amount of time to achieve at least about 90 percent conversion by weight of the monomers. Typically, this time period is in the range of from between about 1 to about 10 hours, or in the range of from 3 to 5 hours.
  • the reaction mixture can be continuously agitated. The following table sets forth approximate broad and narrow ranges for the amounts of the ingredients present in the reaction mixture.
  • the emulsion polymerization reaction yields a latex composition comprising a disperse phase of solid particles and a liquid continuous phase at room temperature.
  • the latex can be a stable colloidal dispersion comprising a disperse phase of high molecular weight polymer particles and a continuous phase comprising water.
  • the polymer particles can make up in the range of from about 10 to about 60 percent by weight of the latex, or in the range of from 40 to 50 percent by weight of the latex.
  • the continuous phase can comprise w r ater, the high HLB surfactant, the hydrate inhibitor (if present), and buffer as needed. Water can be present in the range of from about 20 to about 80 percent by weight of the latex, or in the range of from about 40 to about 60 percent by weight of the latex.
  • the high HLB surfactant can make up in the range of from about 0.1 to about 10 percent by weight of the latex, or in the range of from 0.25 to 6 percent by weight of the latex.
  • the buffer can be present in an amount necessary to reach the pH required for initiation of the polymerization reaction and is initiator dependent. Typically, the pH required to initiate a reaction is in the range of from 6.5 to 10.
  • a hydrate inhibitor When a hydrate inhibitor is employed in the reaction mixture, it can be present in the resulting latex in an amount that yields a hydrate inhibitor-to-water weight ratio in the range of from about 1 :10 to about 10:1, in the range of from about 1 :5 to about 5:1, or in the range of from 2:3 to 3:2.
  • all or part of the hydrate inhibitor can be added to the latex after polymerization to provide the desired amount of hydrate inhibitor in the continuous phase of the latex.
  • the emulsion polymer of the disperse phase of the latex can have a weight average molecular weight ("M w ") of at least about 1 x 10 6 g/mol, at least about 2 x 10 6 g/mol, or at least 5 x 10 6 g/mol.
  • the initial emulsion polymer particles can have a mean particle size of less than about 1 micrometer (" ⁇ m"). in the range of from about 10 to about 500 nanometers ("run"'), or in the range of from 50 to 250 nm.
  • At least about 95 percent by weight of the initial emulsion polymer particles in the latex can be larger than about 10 nm and smaller than about 500 nm. Further, at least about 95 percent by weight of the particles can be larger than about 25 nm and smaller than about 250 nm.
  • the term "consolidated polymer structure" shall denote polymer particles or structures having an increased average particle size compared to the average particle size of the polymer particles prior to consolidation.
  • Consolidation of the initial latex particles can be accomplished by any method known in the art capable of producing consolidated polymer structures. In one embodiment of the present invention, consolidation can be performed using any technique sufficient to produce consolidated polymer structures having an average particle size at least about 5 times, at least about 10 times, or at least 100 times the average particle size of the initial particles prior to consolidation.
  • consolidation of the initial emulsion polymer particles can be accomplished by subjecting the latex to a drying step.
  • Consolidation by drying can be accomplished by any drying method known in the art capable of removing of at least a portion of the continuous phase of the latex described above.
  • the drying technique employed can be sufficient to remove at least about 70 weight percent, at least about 90 weight percent, or at least 95 weight percent of the continuous phase of the latex.
  • the drying technique employed to form the above-mentioned consolidated polymer structures can be spray drying. Spray drying is a method of drying materials having both liquid and solid phases, including such materials as latexes, colloids, and suspensions. Any spray drying method known in the art can be employed as the consolidation technique in the present invention. Additionally, the spray drying technique employed in the present invention can comprise at least two steps: (1) atomization and (2) gas/droplet mixing.
  • the latex can be atomized employing an atomizer.
  • the latex droplets formed by the atomizer can have an average diameter in the range of from about 1 to about 500 ⁇ m, in the range of from about 25 to about 350 ⁇ m, or in the range of from 50 to 200 ⁇ m.
  • the atomizer employed in the present invention can be any atomizer known in the art. Examples of suitable atomizers include, but are not limited to, high-pressure nozzles, two-fluid nozzles, and high-speed centrifugal disks.
  • the resulting droplets can then be contacted with a gas stream to at least partially vaporize the continuous phase of the latex.
  • the gas stream suitable for use in the present invention can be air and/or an inert gas.
  • the temperature of the gas stream can be any temperature sufficient to vaporize at least a portion of the continuous phase of the latex.
  • the flow of the gas stream can be counter-current or co-current with the flow of the atomized latex.
  • the droplet/gas mixing time can be any length of time sufficient to produce consolidated polymer structures having increased particle sizes as discussed above. Additionally, the droplet/gas mixing can be sufficient to remove at least about 70 weight percent, at least about 90 weight percent, or at least 95 weight percent of the continuous phase of the latex.
  • a partitioning agent can be added to the latex prior to and/or during spray drying to control the amount of agglomeration of the polvmer.
  • Any partitioning agent known in the industry for limiting polymer agglomeration can be employed in the present invention.
  • suitable partitioning agents include, but are not limited to, alumina, silica, calcined clay, talc, carbon black, calcium stearate, and/or magnesium stearatc.
  • the amount of partitioning agent employed in the spray drying process can be varied depending on the extent of agglomeration desired.
  • the partitioning agent can be present in an amount in the range of from about 0.1 to about 40 weight percent, in the range of from about 1 to about 30 weight percent, or in the range of from 2 to 25 weight percent based on the combined weight of the latex and partitioning agent.
  • the drying technique employed to form the above-mentioned consolidated polymer structures can be thin-layer drying.
  • the thin-layer drying technique suitable for use in the present invention can be any method known in the art that evaporates at least a portion of the continuous phase of the latex, leaving behind a thin layer of film comprising one or more of the above-mentioned consolidated polymer structures.
  • thin-layer drying of the latex can be achieved by placing the latex into a mold, which can be in the shape of a tray or pan.
  • the latex can then be spread into a thin layer.
  • Any method known in the art capable of creating the desired thickness can be employed for spreading the latex in the mold-
  • the latex can be spread in the mold by various mechanical processes to create the desired thickness. Once spread, the latex can have a thickness of less than about 1 inch, less than about 0.75 inches, or less than 0.5 inches.
  • the pan or tray employed in the present invention can be a moving conveyor-type surface in order to make the drying process continuous.
  • Evaporation of at least a portion of the continuous phase of the latex can be achieved by any method known in the art of thin-layer drying.
  • evaporation can be promoted by forced convection in which dry gas, such as air or nitrogen, is blown over the surface of the latex.
  • evaporation can be achieved by employing a spin coating technique.
  • Spin coating is a process whereby the latex is placed on a substrate and then spun at a high speed. Centripetal acceleration causes the latex to spread leaving behind the above-mentioned thin layer of film.
  • the latex can be heated to promote evaporation of the continuous phase. This can be done by heating the surface on which the thin film is being formed and/or by heating the gas that is being forced across it.
  • the latex can be subjected to vacuum conditions to promote evaporation of the carrier fluid. Regardless of which method is employed, at least about 70 weight percent, at least about 90 weight percent, or at least 95 weight percent of the continuous phase can be evaporated during thin-layer drying.
  • the thickness of the resulting film can vary depending on which method or combination of methods is employed. Additionally, film thickness can be affected by viscosity of the continuous phase and percent solids of the latex, among others. In general, however, the thickness of the resulting one or more consolidated polymer structures (i.e., the "thin layer") formed via thin-layer drying can be in the range of from about 0.001 to about 0.25 inches, in the range of from about 0.005 to about 0.2 inches, or in the range of from 0.01 to 0.15 inches.
  • the drying technique employed to form the above-mentioned consolidated polymer structures can be freeze drying.
  • the fieeze drying technique suitable for use in the present invention can be any freeze drying process known in the art suitable to cause at least a portion of the continuous phase of the latex to sublimate, thereby creating one or more of the above-described consolidated polymer structures.
  • a freeze drying process suitable for use in the present invention can comprise the steps of freezing the latex followed by applying vacuum to the frozen latex.
  • the one or more consolidated polymer structures can be reduced in size.
  • the size reduction process can comprise one or more course and/or fine size reduction steps, as will be discussed in greater detail below.
  • consolidation of the emulsion polymer from the latex can be accomplished by freezing the latex.
  • Formation of the one or more consolidated polymer structures via freezing can be accomplished by reducing the temperature of the latex to below the freezing point of the continuous phase.
  • the freezing process may only need to be performed once, or it can be repeated until the desired one or more consolidated polymer structures are obtained.
  • the term '"freeze/thaw stability denotes the degree to which the polymer portion of a latex can resist coagulation or flocculation when frozen as determined by ASTM method D2243.
  • a latex having a higher freeze/thaw stability can undergo multiple freeze/thaw cycles in order to obtain one or more consolidated polymer structures.
  • the latex of the present invention can have a freeze/thaw stability of less than 5 cycles, less than 3 cycles, or less than 1 cycle. Freezing of the latex may be accomplished by any method known in the art for lowering the temperature of the latex to the desired degree.
  • One exemplary method suitable for use in the present invention involves placing the latex into one or more polymeric enclosures, such as, for example, plastic bags or bottles.
  • Suitable plastics for forming the enclosures include, but are not limited to, high-density polyethylene, nylon, polytetrafluoroethylene, polystyrene, and polyolcfins.
  • the enclosure can then be sealed to prevent loss of the latex and immersed in a coolant bath.
  • the coolant employed in the coolant bath can be any coolant capable of lowering the temperature of the latex to below the freezing point of the continuous phase.
  • a suitable coolant for use in the present invention includes, but is not limited to, liquid nitrogen.
  • Another exemplary method for freezing the latex of the present invention involves placing the latex into molds of a desired size and then lowering the temperature of the latex to the desired degree.
  • another method includes forming the latex into droplets, followed by freezing of the droplets. These methods can facilitate later size reduction of the one or more consolidated polymer structures, discussed below.
  • consolidation of the emulsion polymer in the latex to form the above-mentioned one or more consolidated polymer structures can be accomplished by combining the latex with salt water. This method can be accomplished by adding the latex to salt water over a period of time. Conversely, the salt water can be added to the latex over a period of time.
  • the combination of the latex and the salt water can be accomplished by any known method in the art. For example, the combination can be accomplished by pump, gravity feed, or any other suitable method.
  • the latex/salt water mixture can be continuously stirred during addition.
  • the salt water suitable for use in the present invention can comprise any ionized compound in water. Though not wishing to be bound by theory, it is believed that ionized species cause agglomeration of the latex polymer by interfering with the electrical double layer that stabilizes the latex particles.
  • ionizable compounds suitable for use in the present invention include, but are not limited to, alkali metal, alkaline earth metal, and/or transition metal salts of halides, nitrates, phosphates, sulfates, and/or other anions.
  • the volume ratio of latex-to-salt water can be in the range of from about 1 :2 to about 1 :100. in the range of from about 1 :5 to about 1:50.
  • the concentration of salt in the salt water can be at least about 0.5 weight percent, or at least 5 weight percent.
  • the temperature of the salt water and latex during mixing can be in the range of from about the freezing point of the latex to about 100 0 C.
  • the consolidated polymer structures can be substantially isolated by any methods known in the art for accomplishing solid/liquid separation.
  • the selected isolation technique can be sufficient to remove at least about 70, at least about 90, or at least 95 weight percent of the remaining continuous phase.
  • the consolidated polymer structures can be substantially isolated via decantation. filtration, screening, and/or centrifugation After the one or more consolidated polymer structures have been substantially isolated, they can undergo size reduction as discussed in further detail below.
  • consolidation of the emulsion polymer in the latex to form the above-mentioned one or more consolidated polymer structures can be accomplished by combining the latex with a water-mi scible solvent.
  • This method can be accomplished by adding the latex to the water-miscible solvent over a period of time.
  • the water-miscible solvent can be added to the latex over a period of time.
  • the combination of the latex and the water-miscible solvent can be accomplished by any known method in the art. For example, the combination can be accomplished by pump, gravity feed, or any other suitable method. The resulting mixture can be continuously stirred during addition.
  • the water-miscible solvent suitable for use in the present invention can comprise any water-miscible solvent that is a non-solvent for the polymer particles when mixed with water.
  • the water-miscible solvent can be a non-solvent for the polymer particles even when not mixed with water.
  • water-miscible solvents suitable for use in the present invention include, but are not limited to, Ci to C 4 alcohols, dimethyl formamide, dimethyl acetamide, tetrahydrofuran, sulfolane, nitromethane, furfural, and/or l-methyl-2-pyrrolidinone.
  • the volume ratio of latex -to-water-miscible solvent can be in the range of from about 1 :2 to about 1 : 100, in the range of from about 1 :5 to about 1 :50. or in the range of from 1 : 10 to 1 :25.
  • the temperature of the water-miscible solvent and latex during mixing can be in the range of from about the freezing point of the latex to about the boiling point of the latex or the boiling point of the water-miscible solvent, whichever is lower.
  • the selected isolation technique can be sufficient to remove at least about 70 weight percent, at least about 90 weight percent, or at least 95 weight percent of the remaining continuous phase.
  • the consolidated polymer structures can be substantially isolated via decantation, filtration, screening, and/or centrifugation. After the one or more consolida ⁇ ed polymer structures have been substantially isolated, they can undergo size reduction as discussed in further detail below.
  • consolidation of the emulsion polymer from the latex to form the above-mentioned one or more consolidated polymer structures can be accomplished by a dissolution/precipitation technique.
  • the polymer particles can be dissolved by combining the latex with a solvent for the polymer. After the polymer has been at least partially dissolved, the polymer can be precipitated to form the one or more consolidated polymer structures. In one embodiment, at least about 70 weight percent, at least about 90 weight percent, or at least 95 weight percent of the polymer can be dissolved in the solvent prior to precipitation. Any dissolution/precipitation techniques known in the art can be employed in xhe present invention.
  • the solvent for use in the dissolution/precipitation technique can be a low- volatility solvent.
  • low volatility solvents suitable for use in the present invention include, but are not limited to, tetrahydrofuran and/or toluene.
  • the concentration of latex in the solvent can be less than about 20 weight percent, less than about 15 weight percent, or less than 10 weight percent based on the combined weight of the latex and solvent.
  • any method known in the art for precipitating a solute out of solution can be employed. Suitable precipitation techniques include, but are not limited to, contacting the solution with an alcohol or other non-solvent, or by flashing the solution to remove at least a portion of the volatile components of the solution.
  • flashing denotes a process whereby at least a portion of a solution is vaporized by sudden decrease in pressure and/or increase in temperature.
  • the consolidated polymer structures can be substantially isolated by any methods known in the art for accomplishing solid/liquid separation, provided any solvent and/or continuous phase remains after precipitation.
  • the selected isolation technique can be sufficient to remove at least about 70 weight percent, at least about 90 weight percent, or at least 95 weight percent of the remaining continuous phase and/or solvent.
  • the consolidated polymer structures can be substantially isolated via decantation, filtration, screening, and/or centrifugation. After the one or more consolidated polymer structures have been substantially isolated, they can undergo size reduction as discussed in further detail below.
  • the size of the one or more consolidated polymer structures can be decreased to thereby form modified polymer particles. Any method known in the art for reducing the particle size of a polymer-containing material can be employed in the present invention.
  • the one or more consolidated polymer structures can undergo a multi-stage particle size reduction, including coarse size reduction followed by fine size reduction to form the modified polymer panicles.
  • the procedure employed may result in consolidated polymer structures having relatively large diameters (e.g., greater than 0.75 inches).
  • the one or more consolidated polymer structures can optionally undergo coarse size reduction to form intermediate polymer particles.
  • the one or more consolidated polymer structures can undergo coarse size reduction sufficient to achieve intermediate polymer particles having an average size of less than about 2.5 inches on each side, less than about 1.5 inches on each side, or less than 0.75 inches on each side.
  • Coarse size reduction of the one or more consolidated polymer structures can be achie ⁇ ed by any methods known in the art. Examples of methods suitable for use for coarse size reduction in the present invention include, but are not limited to, pulverizing via impact hammers, grinders and/or choppers. Additionally, the temperature of the one or more consolidated polymer structures can be maintained below the glass transition temperature of the polymer during coarse size reduction.
  • At least a portion of the one or more consolidated polymer structures can be reduced to a finely divided state (i.e., modified polymer particles).
  • a finely divided state when used to describe a particulate material shall denote an average particle size of less than 2,000 ⁇ m.
  • An ⁇ - technique known in the art for reducing the particle size of a polymer can be employed in the present inveniion.
  • at least a portion ⁇ f the one or more consolidated polymei devisctuies can be subject to cryogrinding.
  • cryyogrinding shall denote any process wherebv a polymer is reduced to a finely divided state at cryogenic temperatures.
  • cryogenic temperature e.g., any temperature below the glass transition temperature of the polymer being ground.
  • the temperature of the one or more consolidated polymer structures can be lowered to cryogenic temperatures prior to being reduced to a finely divided state.
  • the reduction in temperature of the consolidated polymer structures can be obtained by contacting the consolidated polymer structures with liquid nitrogen.
  • the resulting low-temperature consolidated polymer structures can then be introduced into a cold mill and ground to achieve the desired particle size.
  • a partitioning agent can be added to the consolidated polymer structures during grinding to help prevent the freshly exposed surfaces of the polymer from sticking together.
  • suitable partitioning agents useful in the present invention include, but are not limited to, alumina, silica, calcined clay, talc, carbon black.
  • the amount of partitioning agent employed in the grinding process can be less than about 35 weight percent, less than about 30 weight percent, or less than 25 weight percent based on the total weight of the consolidated polymer structures and partitioning agent.
  • the one or more consolidated polymer structures can be formed via freezing.
  • the consolidated polymer structures formed via this method can undergo size reduction while still frozen in the continuous phase.
  • the latex can be frozen in a packaging material.
  • This packaging material can optionally undergo size reduction concurrently with the consolidated polymer structures and frozen continuous phase.
  • the frozen latex, including the continuous phase and optionally the packaging material can first be pulverized into intermediate nolymer particles, as described above (e.g., chunks having an average size of less than 2.5 inches on each side). If the latex is freeze-thaw stable as defined above, coarse reduction can occur below the freezing point of the continuous phase of the latex. If the latex is not fieeze-thaw stable, coarse reduction can occur at any reasonable temperature that does not impact product quality.
  • the intermediate polymer particles can be reduced to a finely divided state, employing methods such as those described above, in order to produce modified polymer particles.
  • fine size reduction can be performed at a temperature below the glass transition temperatures of both the polymer and the package material, if present, and at a temperature below the freezing point of the continuous phase of the latex.
  • the above-described one or more consolidated polymer structures can be formed and reduced in size in a concurrent process.
  • the above-described latex containing emulsion polymer particles can be fed into a mill concurrently with a gas stream having a temperature abo ⁇ e that of the latex (e.g.. hot air).
  • the temperature and velocity of the gas stream can be adjusted Io obtain the desired residual moisture content in the resulting modified polymer particles.
  • at least about 70 weight percent, at least about 90 weight percent, or at least 95 weight percent of the continuous phase can be removed during the concurrent formation/reduction process.
  • the resulting modified polymer particles can have a mean particle size in the range of from about 5 to about 800 micrometers, in the range of from about 10 to about 600 micrometers, or in the range of from 20 to 400 micrometers. Additionally, the modified polymer particles can have a particle size distribution where D 1O denotes the particle size for which 10 percent of the total sample volume is smaller and 90 percent is larger, D 50 denotes the particle size for which one-half of the sample volume is larger and one-half is smaller (i.e., median particle size), and D 90 is the particle size for which 90 percent of the total sample volume is smaller and 10 percent is larger.
  • the modified polymer particles can have a Dio particle size in the range of from about 0.5 to about 15 ⁇ m, in the range of from about 1 to about 12 ⁇ m, or in the range of from 2 to 10 ⁇ m.
  • the modified polymer particles can have a D 50 particle size in the range of from about 10 to about 90 ⁇ m. in the range of from about 20 to about 80 ⁇ m, or in the range of from 30 to 70 ⁇ m.
  • the modified polymer particles can have a D ⁇ >o particle size in the range of from aboux 80 to about 170 ⁇ m, in the range of from about 90 to about 160 ⁇ m. or in the range of from 100 to 150 ⁇ m.
  • the resulting modified polymer particles can be dispersed in a carrier fluid for use as a drag reducer.
  • the resulting drag reducer can comprise modified polymer particles in the form of a suspension in a carrier fluid.
  • the modified polymer particles can be combined with a carrier fluid in order to form a drag reducer.
  • drag reducer shall denote a composition that when added to a fluid flowing through a conduit, is effective to reduce pressure loss associated with turbulent flow of the fluid through the conduit.
  • the carrier fluid useful in the present invention can be any liquid that is a for the modified polymer particles.
  • the carrier fluid can comprise water and/or low ? er carbon alcohols (e.g., methanol and/or ethanol).
  • the modified polymer particles and the carrier fluid can be added to a mixing lank and mixed in order to form a drag reducer.
  • the amount of modified polymer particles added to the carrier fluid can be sufficient to form a drag reducer having at least about 5 weight percent polymer, in the range of from about 10 to about 40 weight percent polymer, or in the range of from 15 to 35 weight percent polymer.
  • the carrier fluid can comprise other components to aid in the formation and/or maintenance of the drag reducer. These components can be added to the carrier fluid before, during, and/or after the modified particles are mixed with the carrier fluid. Such components include, but are not limited to. density balancing agents, freeze protection agents, suspension stabilizers, wetting agents, anti-foamiiig agents, and/or thickening agents.
  • Density balancing agents/freeze protection agents useful in the present invention include, but arc not limited to, ethylene glycol and propylene glycol.
  • the amount of density balancing agent/freeze protection agent employed in the present invention can be in the range of from about 10 to about 60 weight percent based on the weight of the carrier fluid.
  • Suspension stabilizers useful in the present invention include, but are not limited to talc, tri-calcium phosphate, magnesium stearate, silica, polyanhydride polymers, sterically hindered alkyl phenol antioxidants, and graphite.
  • the amount of suspension stabilize: employed can be minimized or eliminated where possible to reduce the amount of material in the drag reducer that does not act as a drag-reducing agent.
  • the amount of the suspension stabilizer added can be in the range of from about 0 to about 40 weight percent, in the range of from about 5 to about 25 weight percent, or in the range of from 8 to 12 weight percent based on the weight of the carrier fluid.
  • a wetting agent such as a surfactant may be added to aid in the dispersal of the modified polymer particles.
  • Non-ionic surfactants suitable for use as a wetting agent in the present invention include, but are not limited to. linear secondary alcohol ethoxylates, linear alcohol ethoxylates, and/or alkylphenol exthoxylates.
  • Anionic surfactants suitable for use as a wetting agent in the present invention include, but are not limited to, alkyl benzene sulfonates and/or alcohol ethoxylate sulfates (e.g., sodium lauryl sulfate).
  • the amount of wetting agent added can be in the range of from about 0.01 to about 1 weight percent, or in the range of from 0.01 to 0.1 weight percent, based on the weight of the carrier fluid.
  • a suitable anti-foaming agent can be used.
  • anti-foaming agents suitable for use in the present invention include, but are not limited to, ANTIFOAM products (available from Dow Corning, Midland. Mich.), and BUBBLE BREAKER products (available from Witco Chemical Company, Organics Division).
  • the amount of anti-foaming agent employed can be less than about 1 weight percent, based on the weight of the carrier fluid.
  • a thickening agent can be added to increase the viscosity of the mixture. Typical thickening agents are high molecular weight, water-soluble polymers.
  • Thickening agents useful in the present invention include, but are not limited to, polysaccharides, xanthum gum, carboxymethyl cellulose, hydroxypropyl guar, and/or hydroxyethyl cellulose.
  • the modified polymer particles can be added to the continuous phase of a latex already containing emulsion polymerized polymer particles in order to form a drag reducer.
  • the latex of this embodiment can be prepared as described above.
  • the modified polymer particles can be added to the latex in an amount sufficient to produce a drag reducer containing up to about 25 weight percent modified polymer particles based on the entire weight of the drag reducer.
  • the resulting drag reducer can comprise un-modified emulsion polymer particles (i.e., initial emulsion polymer particles) in the range of from about 10 to about 60 percent by weight of the drag reducer, or in the range of from 40 to 50 percent by weight of the drag reducer.
  • the above-described drag reducers can be added to a hydrocarbon-containing fluid.
  • the resulting treated hydrocarbon- containing fluid can then be transported through a pipeline.
  • the hydrocarbon-containing fluid can comprise a liquid phase hydrocarbon, a non-liquid phase hydrocarbon, and/or a non-hydrocarbon fluid.
  • the hydrocarbon-containing fluid can comprise at least about 50 weight percent of a liquid phase hydrocarbon.
  • the hydrocarbon-containing fluid can comprise crude oil.
  • the resulting treated hydrocarbon-containing fluid can comprise a cumulative amount of the drag reducing polymers sufficient to achieve a reduction in drag associated with the turbulent flow of the hydrocarbon-containing fluid through the pipeline of at least about 5 percent, at least about 10 percent, or at least 15 percent.
  • the treated hydrocarbon-containing fluid can have a cumulative concentration of drag reducing polymers in the range of from about 0.1 to about 500 parts per million by weight ('"ppmw' " ), in the range of from about 0.5 to about 200 ppmw, in the range of from about 1 to about 100 ppmw, or in the range of from 2 to 50 ppmw.
  • at least about 50 weight percent, at least about 75 weight percent, or at least 95 weight percent of the polymer particles from the drag reducer can be dissolved by the hydrocarbon-containing fluid.
  • Two batches (Batch 1 and Batch 2) of drag reducing polymers were prepared by emulsion polymerization employing the following procedure. Polymerization was performed in a 185-gallon stainless steel, jacketed reactor with a mechanical stirrer, thermocouple, feed ports, and nitrogen inlets/outlets. The reactor was charged with 440 lbs of monomer (2-ethylhexyl methacrylate), 565.3 lbs of de-ionized water, 68.3 lbs of
  • Polystep B-5 surfactant, available from Stepan Company of Northfield, Illinois
  • 1.24 lbs of potassium phosphate monobasic pH buffer
  • 0.97 lbs of potassium phosphate dibasic pH buffer
  • 33.2 grams of ammonium persulfate. NH 4 ) I S 2 Og (oxidizer).
  • the monomer and water mixture was agitated at 110 rpm while being purged with nitrogen to remove any traces of oxygen in the reactor and was cooled to about
  • the polymerization reaction was initiated by adding into the reactor 4.02 grams of ammonium iron(II) sulfate, Fe(NH 4 ) I (SO 4 ⁇ -OFbO in a solution of 0.010 M sulfuric acid solution in DI water at a concentration of 1,117 ppm at a rate of 5 g/min. The solution was injected for 10 hours to complete the polymerization. The resulting latex was pressured out of the reactor through a 5-micron bag filter and stored.
  • the resulting drag reducer was a latex containing poly(2-ethylhexyl methacrylate) as the active ingredient.
  • the sample had a solids content of 41.2 percent by mass and a nominal polymer content of 40 percent.
  • the density of the sample was 1.0005 g/mL.
  • the continuous phase was 100% water.
  • the polymer particles of the latex were agglomerated using a thin-layer drying technique. For this procedure, the latex was spread in a thin layer on sheet pans. Employing a fan, room temperature air was blown across the pans overnight to evaporate the continuous phase from the latex. After drying, the resulting agglomerated polymer was manually broken apart with a metal hammer into pieces of agglomerated polymer of suitable size to be cryoground.
  • each batch was subjected to cryogrinding in a hammermill using the following procedure. 850 grams of each batch were combined with 365 grams of calcium stearatc partitioning agent in separate plastic containers and shaken to mix. The containers and their contents were pre-chilled by placing them in dry-ice prior to cryogrinding. Each mixture was then individually placed into dewar flasks and frozen with liquid nitrogen. The mixtures were then separately ground by slowly feeding each mixture to a hammermill over a period of approximately 10 minutes. During grinding, the temperature of the hammermill was kept below the glass transition temperature of the polymer using liquid nitrogen.
  • cryoground drag reducing polymers i.e., modified polymer particles
  • each of the 6 sub-batches prepared in Example 2 was separately suspended in an aqueous carrier fluid according to the following procedure.
  • the cryoground polymer was first sieved in order to eliminate undesired lumps.
  • 434.98 g of de-ionized water, 1 1.48 g of TERGlTOL 15-S-7 (surfactant, available from Dow Corning Corp., Midland, MI), and 3.82 g of ANTIFOAM 1410 (available from Dow Corning Corp., Midland, MI) were mixed into a 1 L plastic container.
  • the mixture was then stirred at 600 rpm for 2 minutes.
  • 230.02 g of the cryoground polymer was added slowly over a period of approximately 3 to 4 minutes while continually stirring the mixture at 600 rpm.
  • cryoground polymer Once all of the cryoground polymer was added, the mixture w r as stirred at 600 rpm for an additional 10 minutes. Next, 19.74 g of AQU D-3334 HEC (hydroxyethylcellulose, manufactured by Aqualon Company) was injected into the suspension using a 50 rnL syringe. The suspension was then stirred at a speed of 5200 rpm for 10 minutes.
  • AQU D-3334 HEC hydroxyethylcellulose, manufactured by Aqualon Company
  • the particle sizes of the cryoground polymer in the suspensions prepared in Example 3 were analyzed employing a BECKMAN COULTER LS Particle Size Analyzer, model LS 230, Small Volume Module. Table 1 below displays the results from the analyses, including the mean particle size. Additionally, particle size distributions are given for each sub-batch, where D 1O denotes the particle size for which 10 percent of the total sample volume is smaller and 90 percent is larger, D 50 denotes the particle size for which one-half of the sample volume is larger and one-half is smaller (i.e., median particle size), and D 90 is the particle size for which 90 percent of the total sample volume is smaller and 10 percent is larger.
  • D 1O denotes the particle size for which 10 percent of the total sample volume is smaller and 90 percent is larger
  • D 50 denotes the particle size for which one-half of the sample volume is larger and one-half is smaller (i.e., median particle size)
  • D 90 is the particle size for which 90 percent of the total sample volume is smaller and 10 percent is
  • emulsion polymers in latex form will have a mean particle size of less than about 1 micrometer.
  • the mean particle size of each of the emulsion polymers after consolidation and size reduction performed in Example 2 is greater than the mean particle size of typical emulsion polymers in latex form.
  • the term "and/or,” when used in a list of two or more items, means that any one of the listed items can be employed by itself or any combination of two or more of the listed items can be employed. For example, if a composition is described as containing components A, B, and/or C, the composition can contain A alone; B alone: C alone; A and B in combination; A and C in combination; B and C in combination; or A, B, and C in combination.
  • the terms “comprising,” “comprises,” and “comprise” are open- ended transition terms used to transition from a subject recited before the term to one or more elements recited after the term, where the element or elements listed after the transition term are not necessarily the only elements that make up the subject.
  • consolidated polymer structure refers to polymer particles or structures having an increased average particle size compared to the average particle size of the polymer particles prior to consolidation.
  • containing,' “contains,' “ and “contain” have the same open-ended meaning as “comprising,” “comprises,” and “comprise” provided above.
  • cryogenic temperature shall denote any temperature below the glass transition temperature of a particular polymer.
  • drag reducer refers to a composition that, when added to a fluid flowing through a conduit, is effective to reduce pressure loss associated with turbulent flow of the fluid through the conduit.
  • emulsion polymer shall denote any polymer prepared via emulsion polymerization.
  • finely divided state when used to describe a particulate material shall denote an average particle size of less than 2,000 ⁇ m.
  • flashing denotes a process whereby at least a portion of a solution is vaporized by sudden decrease in pressure and/or increase in temperature.
  • freeze/thaw stability denotes the degree to which the polymer portion of a latex can resist coagulation or flocculation when frozen as determined by ASTM method D2243.
  • HLB number refers to the hydrophile-lipophile balance of an amphiphilic compound as determined by the methods described by W. C. Griffin in J. Soc. Cosmet. Chem., 1, 311 (1949) and J. Soc. Cosmet. Chem., 5, 249 (1954).
  • high HLB shall denote an HLB number of 7 or more.
  • the term "polymer” refers to homopolymers, copolymers, terpolymers of one or more chemical species.
  • turbulent flow refers to fluid flow having a Reynolds number of at least 2,000.
  • weight average molecular weight refers to the molecular w eight of a polymer calculated according to the following formula: where N, is the number of molecules of molecular weight M 1 .

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Abstract

L'invention porte sur une composition de réduction de traînée comprenant au moins un polymère non poly(alpha-oléfinique) ayant une dimension moyenne de particule se situant dans la plage d'environ 5 à environ 800 micromètres. Le polymère non poly(alpha-oléfinique) peut initialement être formé par polymérisation en émulsion. Les particules de polymère initial peuvent ensuite être au moins partiellement consolidées et puis réduites en dimension et mises en suspension dans un fluide vecteur. La composition de réduction de traînée résultante peut être ajoutée à un fluide contenant un hydrocarbure pour diminuer la perte de charge associée à l'écoulement turbulent du fluide contenant un hydrocarbure dans un conduit.
EP08796916.8A 2007-10-26 2008-07-31 Polymères réducteurs de traînée non poly(alpha-oléfiniques) dispersés Not-in-force EP2190904B1 (fr)

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EP20120156575 EP2457942A1 (fr) 2007-10-26 2008-07-31 Polymères réducteurs de traînée non poly(alpha-oléfiniques) dispersés
EP14163613.4A EP2752439B1 (fr) 2007-10-26 2008-07-31 Polymères réducteurs de traînée non poly(alpha-oléfiniques) dispersés
PL08796916T PL2190904T3 (pl) 2007-10-26 2008-07-31 Dyspersyjne polimery redukujące opory przepływu inne niż polialfaolefiny
DK14163613.4T DK2752439T3 (en) 2007-10-26 2008-07-31 DISPERSED FRICTION REDUCING NON-POLYALPHAOLEFIN POLYMERS

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US11/925,214 US7888407B2 (en) 2007-10-26 2007-10-26 Disperse non-polyalphaolefin drag reducing polymers
PCT/US2008/071708 WO2009055114A1 (fr) 2007-10-26 2008-07-31 Polymères réducteurs de traînée non poly(alpha-oléfiniques) dispersés

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EP14163613.4A Division-Into EP2752439B1 (fr) 2007-10-26 2008-07-31 Polymères réducteurs de traînée non poly(alpha-oléfiniques) dispersés
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US8916626B2 (en) * 2008-07-31 2014-12-23 Lubrizol Specialty Products, Inc. Drag reducing copolymers for cold fluid applications
US20120035297A1 (en) 2010-08-09 2012-02-09 Conocophillips Company Remediation of agglomerated flow improvers
CN103627380B (zh) * 2013-11-08 2016-06-08 中国石油天然气股份有限公司 一种水溶性减阻剂及其制备和应用
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US11608466B2 (en) * 2021-03-26 2023-03-21 Baker Hughes Oilfield Operations Llc Solid drag reduction additive and method of using same
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ES2566956T3 (es) 2016-04-18
US10370502B2 (en) 2019-08-06
CO6390072A2 (es) 2012-02-29
BRPI0807980A2 (pt) 2014-06-24
US20110023972A1 (en) 2011-02-03
MX2009009350A (es) 2009-09-21
WO2009055114A1 (fr) 2009-04-30
PL2752439T3 (pl) 2017-05-31
DK2752439T3 (en) 2017-01-30
US9783644B2 (en) 2017-10-10
CA2679848A1 (fr) 2009-04-30
EP2752439B1 (fr) 2016-10-19
EP2190904B1 (fr) 2016-02-10
US7888407B2 (en) 2011-02-15
ES2611466T3 (es) 2017-05-09
DK2190904T3 (en) 2016-05-17
US20090111714A1 (en) 2009-04-30
EA019423B8 (ru) 2014-04-30
EP2752439A1 (fr) 2014-07-09
PL2190904T3 (pl) 2016-07-29
EP2457942A1 (fr) 2012-05-30
ECSP099752A (es) 2009-12-28
CN101932633A (zh) 2010-12-29
US20180118893A1 (en) 2018-05-03
CN101932633B (zh) 2013-03-13
EA019423B1 (ru) 2014-03-31
PT2752439T (pt) 2017-01-27
CA2679848C (fr) 2013-03-19
EA200971011A1 (ru) 2010-04-30

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